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WO1995012445A1 - Procede et dispositif pour la separation d'un melange - Google Patents

Procede et dispositif pour la separation d'un melange Download PDF

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Publication number
WO1995012445A1
WO1995012445A1 PCT/DE1994/001270 DE9401270W WO9512445A1 WO 1995012445 A1 WO1995012445 A1 WO 1995012445A1 DE 9401270 W DE9401270 W DE 9401270W WO 9512445 A1 WO9512445 A1 WO 9512445A1
Authority
WO
WIPO (PCT)
Prior art keywords
separation phase
mixture
chamber
separated
separation
Prior art date
Application number
PCT/DE1994/001270
Other languages
German (de)
English (en)
Inventor
Bernhard Ulbrich
Heinz Jendrny
Original Assignee
Rhône-Poulenc Rorer GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rhône-Poulenc Rorer GmbH filed Critical Rhône-Poulenc Rorer GmbH
Priority to DK94931492T priority Critical patent/DK0726801T3/da
Priority to JP7512951A priority patent/JPH09504230A/ja
Priority to DE59409093T priority patent/DE59409093D1/de
Priority to EP94931492A priority patent/EP0726801B1/fr
Priority to AT94931492T priority patent/ATE188880T1/de
Priority to CA002165825A priority patent/CA2165825A1/fr
Priority to US08/557,023 priority patent/US5863437A/en
Publication of WO1995012445A1 publication Critical patent/WO1995012445A1/fr
Priority to GR20000400876T priority patent/GR3033182T3/el

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/02—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor with moving adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
    • B01D15/08—Selective adsorption, e.g. chromatography
    • B01D15/10—Selective adsorption, e.g. chromatography characterised by constructional or operational features
    • B01D15/18—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns
    • B01D15/1892—Selective adsorption, e.g. chromatography characterised by constructional or operational features relating to flow patterns the sorbent material moving as a whole, e.g. continuous annular chromatography, true moving beds or centrifugal chromatography

Definitions

  • the present invention relates to a method for separating a mixture having at least two components with the features of the preamble of patent claim 1 and an apparatus for carrying out the method.
  • a separation phase which is usually also referred to as a stationary phase
  • the mixture to be separated and then to add at least one fluid to the phase loaded with the mixture elute.
  • the constituents to be separated are those constituents which can be converted into the gas phase without decomposition, the known separation described above is carried out by gas chromatographic means, ie the mixture to be separated and the one used for elution Fluid are both gases.
  • the separation phase (stationary phase) arranged in a column is also applied after it has been loaded the mixture eluted with a liquid or a liquid mixture.
  • This method can be used not only for the separation of mixtures for the purpose of analysis, but also on an industrial scale for the preparative isolation of correspondingly separated components.
  • the column chromatography procedure can also be used for the purification of substances.
  • the disadvantage of the preparative column-chromatographic procedure described above is that it is not possible to continuously separate and isolate certain constituents from the mixture.
  • the column-chromatographic preparative mode of operation only allows a discontinuous, batch-wise operation, ie first the separation phase loaded with the mixture to be separated must be completely eluted with the fluid and, if necessary, regenerated, in order to then subsequently apply the mixture to be separated again to become.
  • a batch procedure is associated with relatively high costs.
  • the present invention has for its object to provide a method of the type specified, which allows continuous separation of a mixture consisting of at least two components.
  • Separation phase with the mixture to be separated and then the separation phase loaded with the mixture eluted with at least one fluid In a departure from the known method in which the separation phase is arranged stationary in a column, in the method according to the invention the separation phase is transferred from a first station (chamber) in which the mixture to be separated is applied to at least one second station (chamber) in which the separation phase is eluted with the at least one fluid. In other words, in the method according to the invention, the separation phase is subjected to the mixture to be separated in a first step and then spatially separated from the loading state. tion is transferred to at least one elution station, where the corresponding loaded separation phase is then eluted with at least one fluid.
  • the method according to the invention has a number of advantages. It should first be emphasized as a major advantage that the method according to the invention permits continuous operation when separating the mixture, in particular also when separating a multicomponent mixture, and is particularly advantageous if the method according to the invention Processes for isolating larger amounts of individual constituents which are contained in the mixture to be separated are used. This not only leads to a considerable increase in the quantity of individual constituents contained in the mixture, but at the same time also results in a significant increase in production without the need to install complex devices. Because of this, it becomes clear that the method according to the invention covers the costs for the isolation of
  • the method according to the invention allows in each individual station an optimal temperature for the separation and an optimal composition for the separation of the elution fluid used in this station, adapted to the individual component or components to be separated in this station of
  • the separation phase is continuously loaded with the mixture, while the loaded separation phase is then also continuously eluted with the fluid.
  • Such an embodiment of the method according to the invention is characterized by a particularly high product throughput and a high separation performance.
  • any separation phase which is suitable for loading the mixture to be separated and correspondingly from the first station (loading station) into the second station can be used in the method according to the invention
  • the selection of the conveyor belt also depends on the method according to the invention.
  • conveyor belts are used for this purpose, which represent fabrics made of metal fibers, polyalkylene fibers, polyester fibers, polyamide fibers and aromatic polyamide fibers, the mesh values of such conveyor belts preferably varying between 20 mesh and 270 mesh, in particular between 60 mesh and 200 mesh.
  • Such conveyor belts ensure that, on the one hand, there are no undesired changes in the separated individual components due to a chemical change in the material of the conveyor belts and, on the other hand, the fluid used for elution still penetrates the conveyor belt perfectly.
  • the thickness of the solid separation phase to be applied to the conveyor belt in the method according to the invention depends on which separation phase is used, how permeable the separation phase is for the fluid used in the elution and how many constituents the mixture to be separated has.
  • the layer thickness of the separation phase arranged on the conveyor belt usually varies between 0.1 cm and 30 cm, preferably between 2 cm and 15 cm.
  • the mixture to be separated is dissolved, dispersed and / or emulsified with a suitable fluid, in particular an organic solvent. Then this solution, dispersion and / or emulsion is applied to the separation phase.
  • the solid separation phase in the method according to the invention is transported from the first station to the second station by means of a conveyor belt, as described above in one embodiment of the method according to the invention, it is advisable to separate the separation phase with the solution, dispersion and / or spray emulsion.
  • the solution, dispersion and / or emulsion of the mixture to be separated is applied, in particular sprayed, onto the separation phase which is then planar in this embodiment of the method according to the invention, that the solution, dispersion and / or emulsion is applied the thickness of the separation phase seen only wets the outer upper region of the separation phase, so that the mixture to be separated in particular only takes up about 5% to 25% of the separation phase, based on its layer thickness.
  • Such a relatively small penetration of the mixture to be separated into the separation phase ensures that the mixture to be separated is properly separated during the subsequent elution with the fluid, in particular the organic solvent, so that particularly pure fractions of the individual constituents accordingly can be isolated.
  • the separation phase can also be applied to the separation phase in the first station, so that, viewed over its thickness, it is completely wetted with the solution, dispersion and / or emulsion of the mixture to be separated.
  • Another embodiment of the method according to the invention provides that between the first station, in which the separation phase is loaded with the mixture to be separated, and the second station, in which the separation phase with the fluid, in particular the mixture an organic solvent, is eluted, the separation phase is dried.
  • the separation phase when the separation phase is transported from the first station to the second station, the fluid used for the application of the mixture to be separated, in particular organic solvents, is expelled by the continuous drying of the separation phase, so that a dried separation phase accordingly is eluted with the fluid, in particular an organic solvent or solvent mixture, in the second station.
  • a variant of the method according to the invention improves the separation performance and thus leads to particularly pure fractions of the individual components of the mixture.
  • this embodiment variant of the method according to the invention is used whenever the fluid used to prepare the solution, dispersion and / or emulsion of the mixture to be separated cannot be mixed with the fluid used for the subsequent elution in the second station or is compatible.
  • the process according to the invention is to be used to separate mixtures which have more than two constituents or more than two fractions, it is advisable to provide a large number of further stations in connection with the second station after which the second station should be entered ⁇ nenden mixture loaded separation phase and is correspondingly eluted there in each individual station.
  • the number of these further stations depends on the number of components to be separated or those to be separated
  • Fractions If, for example, a mixture which has five constituents or five fractions is separated by the process according to the invention, Five stations are also required for the elution of the separation phase, ie in addition to the second station also four further stations. Generally speaking, this means that the number of elution stations, ie thus the number of the second station and the further stations, corresponds to the number of individual components to be separated and / or the number of fractions to be separated of the mixture to be separated, provided that the mixture according to the invention All components should be separated or all fractions should be separated.
  • the separation phase can be flushed with an inert gas during its transport, so that accordingly a particularly gentle separation and isolation into the individual components of the mixture takes place. Furthermore, the purging with the inert gas prevents explosive gas mixtures from occurring when the application and / or elution is carried out with liquids which evaporate easily and are therefore explosive and / or toxic which correspond to the air present Air-fluid vapor mixtures result. Nitrogen, carbon dioxide and / or noble gases and mixtures of the aforementioned gases are preferably used as inert gases in the process according to the invention.
  • the separation phase after elution and drying can be discarded. Otherwise, however, it is suitable if the separation phase is regenerated and, if necessary, dried after completion of the elution and is then cycled again and reused.
  • This embodiment variant of the method according to the invention is characterized by a high level
  • any material that is also used in conventional preparative column chromatography can be used as the separation phase in the process according to the invention.
  • silica gel, diatomaceous earth and / or aluminum oxide are used in the process according to the invention, the grain size of the aforementioned special separation phases varying between 30 ⁇ m and 500 ⁇ m, depending on the particular separation problem.
  • Is natural product Individual components or predetermined fractions can then be isolated particularly quickly, economically and with high purity from such a natural substance extract by using the method according to the invention.
  • a plant extract is used as the mixture to be separated in the process according to the invention, although it is of course also possible to use such an extract which was obtained by extracting animal constituents, for example eggs or the like.
  • a particularly suitable embodiment of the method according to the invention provides that in the method according to the invention an extract, obtained by extracting components of the yew plant, preferably obtained by extracting yew needles or bark of the yew, is used as the mixture to be separated. It was found that a desired individual component, in particular 10-deacetylbaccatin III, can be obtained from such a multicomponent mixture by using the process according to the invention with a high purity, in particular in a purity of more than 80% by weight. and preferably between 92% by weight and 98% by weight, can be isolated particularly economically and gently, which is not the case with the known column chromatography method.
  • the extract mentioned above is obtained as a mixture to be separated, it is obtained from components of the yew plant and preferably from
  • Yew needles, together with a solvent, in particular butyl acetate, are applied to the separation phase and sprayed on in particular. It is advisable here that the extract used and containing butyl acetate contains the 10-dacetylbaccatin III (10-DAB) in a concentration between 3% by weight and 20% by weight, so that after the separation the process according to the invention produces a high-purity 10-deacetylbaccatin III (10-DAB) which has less than 20% by weight and in particular less than 8% by weight to 2% by weight of impurities.
  • 10-DAB 10-dacetylbaccatin III
  • silica gel is preferably used as the separation phase and an alcohol and / or an alcohol mixture is used as the elution fluid. insbeson particular a C- j _-C 4 alcohol and / or a C ⁇ -C ⁇ -alcohol mixture, is used.
  • the process according to the invention is also particularly suitable when the mixture to be separated is crude lecithin, in particular crude lecithin obtained from soybeans.
  • certain individual constituents or fractions of individual constituents can be isolated from crude lecithin or pure lecithin, as will be described in more detail below using specific exemplary embodiments.
  • Soy lecithin a mixture understood the following
  • Composition has:
  • glycolipids 5 - 10% by weight glycolipids
  • the de-oiled crude lecithin also used as a mixture in the process according to the invention, which is also referred to as pure lecithin or lecithin granules, has a phosphatidylcholine content which varies between 15% by weight and 35% by weight, while otherwise with Except for the oil concentration mentioned above, the other constituents (phosphatidylethanolamine, phosphatidylinositol, phosphatidic acid, N-acylphosphatidylethanolamine, other phospholipids) are in the mass ratios given above for crude lecithin.
  • This lecithin (raw or pure lecithin) can then be used, for example, by using the The process according to the invention, depending on the process parameters used in each case, in particular the separation phase used, the temperature, the transport speed of the separation phase, the solvent used for the elution and / or the layer thickness of the separation phase, not only individual products, such as phospholipids with a Concentration of at least 90% by weight of phosphatidylcholine, but also certain fractions defined in their composition, such as in particular fractions which are isolated
  • phosphatidic acid 0-10% by weight phosphatidic acid, 0-5% by weight oil and
  • an alcohol and / or an alcohol mixture preferably a C 1 -C 4 alcohol and / or a C 1 -C 4 alcohol mixture
  • the elution fluid is used as the elution fluid , used.
  • the temperature to be used in the method according to the invention it should be noted that the method according to the invention in particular enables any temperature setting in the individual stations, this temperature setting then depending on the mixture to be separated and the solution used for the elution ⁇ means is matched.
  • the temperature during the elution usually varies between 10 ° C. and 60 ° C., preferably between 20 ° C. and 35 ° C.
  • the present invention further relates to a device for carrying out the method according to the invention described above.
  • the device according to the invention for carrying out the method according to the invention described above has a first chamber (1st station) for applying the mixture to be separated to a separation phase and at least one second chamber (2nd station) for eluting the separation phase loaded with the mixture , wherein the first and the second chamber are provided with a conveyor for transporting the separation phase from the first chamber into the second chamber.
  • the device according to the invention has a number of
  • the device according to the invention has a relatively simple and compact design, which has the consequence that the device according to the invention can be produced relatively inexpensively.
  • the at least two chambers in which the separation phase is loaded with the mixture to be separated (first chamber) or in which the elution of the loaded which separation phase is carried out with the fluid (second chamber) is designed as a closed system, so that all fluids can be used in the device according to the invention, for example also fluids which are toxic or which are explosive air with air - Form fluid vapors.
  • the conveyor device is designed as a conveyor belt, preferably as an endless conveyor belt.
  • the separation phase is preferably loaded continuously in the first chamber with the mixture to be separated, preferably with a solution, dispersion and / or emulsion of the mixture to be separated, and then continuously transported into the second chamber, where the elution, preferably the elution phase is also continuously eluted with the fluid used for this purpose.
  • a particularly suitable embodiment of the device according to the invention has an application device for a corresponding liquid phase (solution, dispersion and / or or emulsion of the mixture to be separated in the first chamber or elution liquid in the second chamber), this application device being positioned stationary and above the separation phase.
  • this application device can be of any design, and particularly reproducible results can be achieved when applying the mixture to be separated to the separation phase or when eluting the separation phase loaded with the mixture if the application device is designed as an application nozzle which extends across the entire width of the conveyor of the separation phase.
  • a further embodiment of the device according to the invention which is also used in particular for the separation of such mixtures from which a plurality of constituents and / or fractions are to be isolated, has one to eight further chambers which, as seen in the conveying direction, separate the separation phase the second chamber are arranged.
  • the separation phase loaded with the mixture is first eluted with a first fluid, preferably continuously eluted, so that when the separation phase is transported into the first further chamber, a further elution of the separation phase to isolate a second component or a second component Fraction can take place.
  • a first fluid preferably continuously eluted
  • one of the further chambers is designed as a drying chamber, this drying chamber preferably being seen in the direction of transport of the separation phase End of the device is located.
  • this drying chamber which can be heated in particular to a temperature between 50 ° C. and 180 ° C., preferably between 80 ° C. and 130 ° C., suction devices through which the drying chamber is arranged are arranged to accelerate the removal of the fluids can be subjected to a vacuum.
  • a further embodiment of the device according to the invention which is also used in particular for the separation of mixtures from which a plurality of constituents and / or fractions are to be isolated, has one to eight further chambers, which, seen in the direction of conveyance of the separation phase, follow the second Chamber are arranged.
  • the separation phase loaded with the mixture is first eluted with a first fluid. iert, preferably continuously eluted, so that when the separation phase is transported into the first further chamber, a further elution of the separation phase can be carried out to isolate a second component or a second fraction. Analogue then takes place in the second to eighth chamber.
  • another embodiment of the invention provides device according to the invention that, seen in the transport direction of the separation phase, one in front of the first chamber
  • the application device is preferably designed in such a way that a dispersion of the separation phase is rinsed onto the conveyor belt with a continuous amount per unit area of conveyor belt, so that the dispersing agent, which is preferably water and / or especially ethanol, can escape and thus a solid separation phase is formed on the conveyor belt.
  • the dispersing agent which is preferably water and / or especially ethanol
  • a drying chamber can additionally be arranged in front of the first chamber.
  • the application device in this way, for example in the form of a slit extending across the width of the conveyor belt, which is used to apply a dry, solid separation phase directly to the conveyor belt.
  • a further embodiment of the device according to the invention has a drying chamber which is positioned in the transport direction of the separation phase between the first chamber and the second chamber.
  • Drying chamber can be designed, as described above for the drying chamber, which is used to separate the eluted separation phase.
  • a fluid which is used for elution is preferably a liquid, in particular an organic solvent, and in the case of the special applications of the process according to the invention for the separation of natural product extracts described above, the alcohols or alcohol mixtures specifically mentioned there are used as eluents.
  • tion fluid can be used.
  • the embodiment of the device designated overall by 1 in the single figure of the drawing has a first chamber 2, a second chamber 3 and a further chamber 4, an endless conveyor belt 5 extending from the inlet 6 of the first chamber 2 to extends to the outlet 7 of the further chamber 4.
  • Each of the chambers 2, 3 and 4 are connected to a drain opening 8, 9 and 10, respectively, where at the discharge openings 8 to 10 open into corresponding tanks, which are not shown.
  • the endless conveyor belt 5 is loaded with a separation phase 11 at the inlet 6 of the first chamber 2 via an application device (not shown), the application device (not shown) being designed such that the separation phase 11 is applied to the conveyor belt 5 in the dry state becomes.
  • the layer thickness and the bulk density of the separation phase 11 can be adjusted.
  • the separation phase continuously transported in the direction of arrow 12 by means of the conveyor belt 5 is sprayed with the solution, dispersion and / or emulsion of the mixture to be encountered via corresponding metering nozzles 13, said metering nozzles 13 across the entire width of the separation phase 11 extend.
  • the chamber 3 has three nozzle devices 14, shown by way of example, which extend transversely to the transport direction of the separation phase 11 and which cause an elution of an individual component or a fraction from the mixture.
  • the constituent or fraction of the mixture contained in the eluent is obtained at the discharge opening 9 and can be temporarily stored in the tank (not shown) and worked up accordingly.
  • the separation phase 11 is placed under vacuum and heated, which has the consequence that all residues of the eluent are removed.
  • a 50% by weight solution of mixture A in ethanol was treated on the device described above.
  • Aluminum oxide was provided as a separation phase in a layer thickness of 8 cm, the conveyor belt being 1 m wide and being transported through the chambers 2 to 4 at a speed of 10 m / h.
  • the separation phase loaded with mixture A was sprayed with 700 kg ethanol / h.
  • composition B (before treatment) 77-86% by weight phosphatidylcholine 0-4% by weight phosphatidylethanolamine 0-4% by weight phosphatidylinositol 3-6% by weight phosphatidic acid 1-5% by weight soybean oil 0-19% by weight others
  • Composition Mixture B (after treatment) 77-86% by weight phosphatidylcholine
  • the ethanol-moist separation phase in the drying chamber 4 was heated to a temperature of 80 ° C. under vacuum, which resulted in the ethanol being completely expelled from the separation phase and thus a dry separation phase which was correspondingly discarded. was incurred.
  • a 20% by weight solution of mixture C in ethanol was treated on the device described above.
  • Aluminum oxide was provided as a separation phase in a layer thickness of 8 cm, the conveyor belt being 1 m wide and being transported through the chambers 2 to 4 at a speed of 10 m / h.
  • the first chamber 2 2,250 kg of the 20% by weight solution of the mixture A in ethanol / h were sprayed onto the separation phase and suctioned off continuously.
  • the separation phase loaded with the mixture C was rinsed with 1,000 kg of ethanol / h.
  • the resulting eluate and drawn off via the discharge openings 8 and 9 contained a mixture D, the composition of the mixtures C and D being reproduced below.
  • Composition mixture C (before treatment)
  • soybean oil 1 - 5% by weight of soybean oil
  • Composition mixture D (after treatment)
  • soybean oil 1 - 3% by weight soybean oil
  • the concentration of other accompanying substances was considerably reduced.
  • the ethanol-moist separation phase in the drying chamber 4 was heated to a temperature of 80 ° C. under vacuum, which resulted in the ethanol being completely expelled from the separation phase and thus a dry separation phase which was correspondingly discarded. was incurred.
  • the separation phase loaded with the mixture E was rinsed with 1,000 kg of ethanol / h.
  • the resulting eluate and drawn off via the discharge opening 9 contained a mixture F, the composition of the mixtures E and F being reproduced below.
  • Composition Mixture E (before treatment) 45-55% by weight phosphatidylcholine
  • Composition Mixture F (after treatment) 70 - 80% by weight phosphatidylcholine 0 - 12% by weight phosphatidylethanolamine 0 - 6% by weight phosphatidylinositol 0 - 1% by weight phosphatidic acid 1 - 3% by weight soybean oil 0 - 8% by weight others Accompanying substances.
  • the ethanol-moist separation phase in the drying chamber 4 was heated to a temperature of 80 ° C. under vacuum, which resulted in the ethanol being completely expelled from the separation phase and thus a dry separation phase which was correspondingly discarded. was incurred.
  • a 50% by weight solution of the mixture G in ethanol was treated on the device described above. Silicon dioxide with a layer thickness of 12.5 cm was provided as the separation phase, the conveyor belt having a width of 1 m and being transported through the chambers 2 to 4 at a speed of 10 m / h.
  • the separation phase loaded with the mixture G was sprayed with 2,000 kg of ethanol / h.
  • the separation phase loaded with the mixture was eluted with 7,000 kg of ethanol.
  • the resulting eluate and drawn off via the discharge opening 10 contained a mixture H, the composition of the mixtures G and H being reproduced below.
  • Composition Mixture G (before treatment) 16-36% by weight phosphatidylcholine 0-20% by weight phosphatidylethanolamine 0-8% by weight phosphatidylinositol 3-10% by weight phosphatidic acid 25-40% by weight soybean oil 0-6% by weight others Accompanying substances
  • Composition mixture H (after treatment)
  • the ethanol-moist separation phase was heated in the drying chamber 4 under vacuum to a temperature of 80 ° C, which resulted in that
  • a 70% solution of a dried extract obtained by extracting yew needles with methanol was prepared in butyl acetate and treated on the device described above.
  • silica gel (Compalox) was provided as a separation phase in a layer thickness of 10 cm on the conveyor belt, the conveyor belt being 1 m wide and being transported through the chambers 2 to 4 at a speed of 5 m / h.
  • the separation phase loaded with the mixture was sprayed with 300 kg of methanol / h.
  • the separation phase loaded with the mixture was eluted at 30 ° C. + 5 ° C. with a solvent mixture (methanol: acetone: ethyl acetate; V: V: V; 70%: 15%: 15%), the Throughput of this solvent mixture was 500 kg per hour.
  • a solvent mixture methanol: acetone: ethyl acetate; V: V: V; 70%: 15%: 15%
  • the resulting eluate and drawn off from the chamber 4 via the discharge opening 10 consisted mainly of 10-deacetyl-baccatin III (10-DAB) in addition to the solvent reproduced above, the 10-deacetylbaccatin III having a purity of 97% by weight.
  • the 70% starting solution of the extract which was applied and to be separated in the first chamber in embodiment 5 had a maximum of between 4% and 5% by weight of 10-diacetylbaccatin III (10-DAB).

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  • Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Centrifugal Separators (AREA)
  • Fats And Perfumes (AREA)
  • Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
  • Compositions Of Macromolecular Compounds (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)

Abstract

Procédé et dispositif pour la séparation d'un mélange renfermant au moins deux constituants. Selon ledit procédé, une phase de séparation est admise avec le mélange à séparer, après quoi la phase de séparation chargée du mélange est éluée par au moins un fluide. La phse de séparation est transportée, à partir d'un premier poste où elle est introduite avec un mélange à séparer, vers au moins un deuxième poste où la phase de séparation est éluée par au moins un fluide.
PCT/DE1994/001270 1993-11-02 1994-10-27 Procede et dispositif pour la separation d'un melange WO1995012445A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
DK94931492T DK0726801T3 (da) 1993-11-02 1994-10-27 Fremgangsmåde til adskillelse af en blanding
JP7512951A JPH09504230A (ja) 1993-11-02 1994-10-27 混合物の分離のための方法及び装置
DE59409093T DE59409093D1 (de) 1993-11-02 1994-10-27 Verfahren zum auftrennen eines gemisches
EP94931492A EP0726801B1 (fr) 1993-11-02 1994-10-27 Procede pour la separation d'un melange
AT94931492T ATE188880T1 (de) 1993-11-02 1994-10-27 Verfahren zum auftrennen eines gemisches
CA002165825A CA2165825A1 (fr) 1993-11-02 1994-10-27 Methode et dispositif pour la separation d'un melange
US08/557,023 US5863437A (en) 1993-11-02 1994-10-27 Method and device for the separation of a mixture
GR20000400876T GR3033182T3 (en) 1993-11-02 2000-04-11 Process and device for separating a mixture

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DEP4337289.9 1993-11-02
DE4337289 1993-11-02

Publications (1)

Publication Number Publication Date
WO1995012445A1 true WO1995012445A1 (fr) 1995-05-11

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PCT/DE1994/001270 WO1995012445A1 (fr) 1993-11-02 1994-10-27 Procede et dispositif pour la separation d'un melange

Country Status (11)

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US (1) US5863437A (fr)
EP (1) EP0726801B1 (fr)
JP (1) JPH09504230A (fr)
AT (1) ATE188880T1 (fr)
CA (1) CA2165825A1 (fr)
DE (2) DE59409093D1 (fr)
DK (1) DK0726801T3 (fr)
ES (1) ES2144533T3 (fr)
GR (1) GR3033182T3 (fr)
PT (1) PT726801E (fr)
WO (1) WO1995012445A1 (fr)

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AUPQ025599A0 (en) * 1999-05-10 1999-06-03 Uniquest Pty Limited Apparatus and method to at least partially separate components from a fluid feed stream
US7285219B2 (en) * 2004-08-10 2007-10-23 Prime Separations, Inc. Chromatographic separation member and method
JP5783939B2 (ja) * 2012-03-14 2015-09-24 株式会社東芝 リン回収装置
DE102015108860A1 (de) * 2015-06-03 2016-12-08 Thyssenkrupp Ag Verfahren und Vorrichtung zur Durchführung von Stoffaustauschvorgängen, Stofftrennvorgängen und/oder Reaktionen unter Beteiligung mindestens einer stationären und mindestens einer mobilen Phase

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ES2144533T3 (es) 2000-06-16
EP0726801B1 (fr) 2000-01-19
PT726801E (pt) 2000-06-30
GR3033182T3 (en) 2000-08-31
DK0726801T3 (da) 2000-05-01
CA2165825A1 (fr) 1995-05-11
DE4438402A1 (de) 1995-05-04
EP0726801A1 (fr) 1996-08-21
US5863437A (en) 1999-01-26
DE59409093D1 (de) 2000-02-24
ATE188880T1 (de) 2000-02-15

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